EP1078677A2 - Procédé et dispositif pour règler la concentration d'un melange gazeux - Google Patents

Procédé et dispositif pour règler la concentration d'un melange gazeux Download PDF

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Publication number
EP1078677A2
EP1078677A2 EP00115109A EP00115109A EP1078677A2 EP 1078677 A2 EP1078677 A2 EP 1078677A2 EP 00115109 A EP00115109 A EP 00115109A EP 00115109 A EP00115109 A EP 00115109A EP 1078677 A2 EP1078677 A2 EP 1078677A2
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EP
European Patent Office
Prior art keywords
gas
line
pressure
permeate
separation membrane
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP00115109A
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German (de)
English (en)
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EP1078677B1 (fr
EP1078677A3 (fr
Inventor
Naohiko Harima Technical Center of Yamashita
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude
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Publication of EP1078677A2 publication Critical patent/EP1078677A2/fr
Publication of EP1078677A3 publication Critical patent/EP1078677A3/fr
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Publication of EP1078677B1 publication Critical patent/EP1078677B1/fr
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B01D53/225—Multiple stage diffusion
    • B01D53/226—Multiple stage diffusion in serial connexion
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/025—Preparation or purification of gas mixtures for ammonia synthesis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/501—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis in the gas phase
    • C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C01C1/0482—Process control; Start-up or cooling-down procedures
    • G—PHYSICS
    • G05—CONTROLLING; REGULATING
    • G05D—SYSTEMS FOR CONTROLLING OR REGULATING NON-ELECTRIC VARIABLES
    • G05D11/00—Control of flow ratio
    • G05D11/02—Controlling ratio of two or more flows of fluid or fluent material
    • G05D11/035—Controlling ratio of two or more flows of fluid or fluent material with auxiliary non-electric power
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0405—Purification by membrane separation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/048—Composition of the impurity the impurity being an organic compound
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the present invention relates to a concentration regulating method and a concentration regulating apparatus for carrying out the concentration regulation of a mixed gas by gas separation, and particularly to a useful technique of decreasing the concentration of a hardly permeable gas as in such a case that the concentration of a mixed gas consisting of nitrogen gas and hydrogen gas is regulated to produce a feed material for ammonia synthesis.
  • a technique of carrying out the purification of a mixed gas by utilization of a gas separation membrane has been hitherto known, and the mechanism and principle thereof are as follows.
  • a gas separation membrane made of a material different in permeability to the respective components of a mixed gas as a feed material is used, namely, the mixed gas fed as it is pressurized is separated to a permeate gas which is permeated through the same gas separation membrane and a retentate gas which is retained on the feed side.
  • a difference (a difference in partial pressure) between one (a gas partial pressure) obtained by multiplying the whole pressure of the feed side (the high pressure side) by the mole fraction of each gas component and the other (a gas partial pressure) obtained by multiplying the whole pressure of the permeation side (the low pressure side) by the mole fraction of the same gas component becomes a motive power of permeation, and the permeation of each gas component is caused at a ratio obtained by multiplying this difference in partial pressure by a permeability and a membrane area.
  • the gas separation accordingly, an easily permeable gas higher in permeability and a hardly permeable gas lower in permeability are separated as they are concentrated on the permeation side and on the feed side (the retentate gas side), respectively.
  • the concentration of a hardly permeable gas can be decreased, for instance, by leading out a part of a mixed gas as a feed material and separating it to a permeate gas and a retentate gas by a gas separation membrane, and then introducing the permeate gas, in which an easily permeable gas has been concentrated, into the mixed gas again.
  • the concentration of an easily permeable gas in a retentate gas is lower and the higher the recovery of the easily permeable gas is, the higher the efficiency of gas separation is, and this becomes an important factor in a case where a compensation to the loss of the easily permeable gas is higher.
  • the concentration of the easily permeable gas in a permeate gas is extremely lower, although it is not so important, on the other hand, the hardly permeable gas become apt to be entrained in the permeate gas and this is disadvantageous because a power for the gas separation therefore increases.
  • a mixed gas as a feed material is produced by another process, and it has, for example, a whole pressure of about 25 bar (absolute pressure, this unit will apply to the following), in which the mole ratio of nitrogen gas exceeds a mole ratio (1/3) suitable for ammonia synthesis, and hence the concentration of nitrogen gas must be decreased. Since it is required in an ammonia synthesis process that the feed pressure of a mixed gas is generally 60 ⁇ 200 bar, on the other hand, the pressure thereof is raised to the same pressure in turn by a first booster C11 and a second booster C12. In this example, the pressure raising is performed to 50 bar in the first stage and to 100 bar in the second stage.
  • the permeate gas is introduced into the inlet side line of the first booster C11 so as to be joined with the feed material mixed gas.
  • the retentate gas in which hardly permeable nitrogen gas has been concentrated, is discharged out of the system and removed from the mixed gas, and hence the concentration of the hardly permeable gas in the mixed gas can be decreased.
  • a mixed gas having a desired mole ratio can be obtained.
  • the mixed gas concentration regulating method comprises feeding a mixed gas consisting of two or more gases different in permeability to a gas separation membrane to a line having a booster so that the pressure thereof is raised, leading out a part of the mixed gas from said pressure raising line and separating it to a permeate gas and a retentate gas by a gas separation membrane, and then introducing said permeate gas into said pressure raising line, thereby regulating the concentration of the mixed gas, and is characterized in that the gas led out of said pressure raising line is separated to a first permeate gas and a first retentate gas by a first gas separation membrane, and then the first retentate gas is separated to a second permeate gas and a second retentate gas by a second gas separation membrane, and said first permeate gas and said second permeate gas are introduced into the pressure raising line separately or after they are joined, and the pressure ratio (the feed side/the perme
  • said gas separation membrane is composed of three or more stages, where a retentate gas of the preceding stage is separated in turn by a gas separation membrane of the succeeding stage, and permeate gases in the respective stages are introduced into said pressure raising line separately or after they are joined, and that the pressure ratio (the feed side/the permeation side) on the feed side and permeation side is made larger as in the gas separation membrane of the latter stage side (the invention described in claim 2).
  • stage number in the present invention is indicative of the number of connection units in a case where units (gas separation sections or gas separation membranes) for performing the gas separation, are connected in series, and each of the units may be a group of gas separation sections or membranes, in which the gas separation sections or membranes are connected in parallel.
  • the mixed gas concentration regulating method comprises raising the pressure of a mixed gas consisting of two or more gases different in permeability to a gas separation membrane in turn by a first booster and a second booster, separating a gas partially led out of the outlet side line of said second booster to a first permeate gas and a first retentate gas by a first gas separation membrane, and then separating said first retentate gas to a second permeate gas and a second retentate gas by a second gas separation membrane, and introducing said first permeate gas into the inlet side line of said second booster and introducing said second permeate gas into the inlet side line of said first booster, and in which the pressure ratio (the feed side/the permeation side) on the feed side and permeation side in the second gas separation membrane is preferably made larger than the pressure ratio (the feed side/the permeation side) on the feed side and permeation side in the first gas separation membrane (the invention described in claim 3).
  • the mixed gas as a feed material consists of nitrogen gas and hydrogen gas, where the mole ratio thereof (nitrogen gas/hydrogen gas) preferably exceeds 1/3 (the invention described in claim 4).
  • the mixed gas concentration regulating apparatus comprises a pressure raising line having a booster for raising the pressure of a mixed gas consisting of two or more gases different in permeability to a gas separation membrane, a line for leading out a part of the mixed gas from said pressure raising line, a gas separation section for separating the gas fed from said line to a permeate gas and a retentate gas by a gas separation membrane, and a line for introducing said permeate gas into said pressure raising line, and is characterized in that said gas separation section is composed of plural stages, where respective stages are connected with each other by a line for feeding a retentate gas of the preceding stage to a gas separation membrane of the succeeding stage and a line is provided for introducing permeate gases of the respective stages into said pressure raising line separately or after they are joined, and another booster is provided or the pressure difference of said pressure raising line is utilized so that the pressure ratio (the feed side/the permeation side) on the feed side and permeation side is made larger as
  • the mixed gas concentration regulating apparatus preferably comprises a first booster and a second booster for raising the pressure of a mixed gas consisting of two or more gases different in permeability to a gas separation membrane in turn, a line for leading out a part of the mixed gas from the outlet side line of said second booster, a first gas separation section for separating the gas fed from said line to a first permeate gas and a second retentate gas by a first gas separation membrane, a line for feeding said first retentate gas to a second gas separation section, a second gas separation section for separating the gas fed from said line to a second permeate gas and a second retentate gas by a second gas separation membrane, a line for introducing said first permeate gas into the inlet side line of said second booster, and a line for introducing said second permeate gas to the inlet side line of said first booster (the invention described in claim 6).
  • a gas separation section is composed, in any case, of plural stages (in series) and the pressure ratio (the feed side/the permeation side) on the feed side and permeation side is made lager as in the gas separation section of the latter stage side, and hence the power expense can be more restrained as the recovery of an easily permeable gas is maintained. Namely, since the concentration of an easily permeable gas is higher as in the gas separation section of the former stage side, a large amount of the easily permeable gas can be recovered with a small pressure drop even at a relatively small pressure ratio and the power expense of the former stage side can be restrained.
  • two boosters for raising the pressure of a mixed gas as a feed material are used to give the pressure ratio, as mentioned above, and hence there is no need of providing another booster and the equipment expense can be more decreased.
  • a mixed gas as a feed material consists of nitrogen gas and hydrogen gas, and hence its separation carried out by a gas separation membrane becomes easy. Furthermore, hardly permeable nitrogen gas can be removed from a mixed gas, in which the mole ratio of nitrogen gas/hydrogen gas thereof exceeds 1/3, and at the same time the pressure raising of the mixed gas can be carried out, and hence a mixed gas suitable as a feed material for ammonia synthesis can be properly produced.
  • This embodiment is an example of carrying out, by use of such an apparatus shown in Fig. 1, the concentration regulation of a mixed gas consisting of nitrogen gas and hydrogen gas as main components, which is a feed material, so that the concentration of nitrogen gas is lowered, where it is intended to make compatible the maintenance of the recovery of hydrogen gas and the restraint of the power expense, with restraining the equipment expense of boosters due to the use of a booster for double purpose.
  • a mixed gas as a feed material is one produced in another step, and it is, for example, one having a whole pressure of about 25 bar, in which the mole ratio of nitrogen gas exceeds 1/3.
  • a product gas has a pressure meeting with an ammonia synthesis process.
  • a mixed gas of about 25 bar is therefore raised in pressure in turn to about 50 bar by a first booster C11 and to about 100 bar by a second booster C12.
  • a centrifugal compressor is properly used and one capable of carrying out two-stage compression at a compression ratio of 2 will be preferable.
  • a water-cooled cooler for temperature maintenance use is provided just after each of the boosters, but it is omitted in the drawings.
  • a booster for double purpose as a booster for raising the pressure of a product gas and a booster for generating a pressure difference for gas separation.
  • two-stage gas separation will be carried out in accordance with the following steps.
  • a gas partially led out of the outlet side line of said second booster C12 is fed to a first gas separation section S1 via a line L1 and separated to a first permeate gas and a first retentate gas by a first gas separation membrane M1 provided in the inside thereof.
  • the first retentate gas is fed to a second gas separation section S2 via a line L3 and separated to a second permeate gas and a second retentate gas by a second gas separation membrane M2 provided in the inside thereof.
  • the first permeate gas is introduced into the inlet side line of the second booster C12 (midway of the first and second boosters C11 & C12) via a line L,Q and the second permeate gas is introduced into the inlet side line (the feed material feed line) of the first booster C11 via a line L,S so that they are joined with the feed material mixed gas.
  • the concentration of the hardly permeable gas in the mixed gas can be decreased, whereby a mixed gas having a desired mole ratio can be obtained.
  • the pressure ratio (the feed side/the permeation side) on the feed side and permeation side in the second gas separation membrane M2 is generated by two boosters and the pressure ratio (the feed side/the permeation side) in the first gas separation membrane M1 is generated by one booster, and the pressure ratio of the former becomes therefore larger than that of the latter.
  • the gas separation section having the gas separation membrane there is properly used a membrane module, in which an element equipped with a gas separation membrane is incorporated in a pressure container, and which is constructed in such a structure that a flow passage from the feed side to the retention side (the outlet side) and a flow passage on the permeation side are isolated with the gas separation membrane.
  • a membrane module in which an element equipped with a gas separation membrane is incorporated in a pressure container, and which is constructed in such a structure that a flow passage from the feed side to the retention side (the outlet side) and a flow passage on the permeation side are isolated with the gas separation membrane.
  • module types for use in the gas separation such as a hollow fiber type and a spiral type.
  • gas separation membrane there will be used various membranes made of polyamide, polyimide, polyamideimide, polyester, polycarbonate, polysulfone, polyethersulfone, polyetherketone or blends thereof.
  • a gas separation membrane there are exemplified a hollow fiber and flat membrane and there can be properly used a membrane having an asymmetric structure.
  • these separation membranes there can be used various kinds of membranes available in market.
  • the materials of gas separation membranes in the respective stages may be the same or different in kind.
  • a gas separation membrane module for hydrogen manufactured by MEDAL Co.
  • MEDAL Co. a gas separation membrane module for hydrogen
  • An example of concretely carrying out the concentration regulation by use of this membrane module will be described, as compared with conventional methods.
  • impurities such as methane, argon and moisture are contained in a practical feed gas, in addition, these components are disregarded for simplification of the discussion, where the concentrations of residual components other than the concentration of hydrogen gas will be dealt with as the concentration of nitrogen gas.
  • the membrane area of the first gas separation membrane M1 was made equal to 2 units of the 12 inch type module and the membrane area of the second gas separation membrane M2 was made equal to 4 units of the 12 inch type module, the gas separation was operated at the aforementioned set pressures.
  • the data shown in Table 1 was obtained.
  • the conventional method 1 was carried out by an apparatus shown in Fig.4 and could be grasped as a special example where the area of the first gas separation membrane was 0 (zero), and hence it was expressed as in Table 1.
  • the area of the gas separation membrane became 4.43.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Automation & Control Theory (AREA)
  • Combustion & Propulsion (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Power Engineering (AREA)
  • Physics & Mathematics (AREA)
  • General Physics & Mathematics (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
EP00115109A 1999-08-27 2000-07-12 Procédé pour règler la concentration d'un melange gazeux Expired - Lifetime EP1078677B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP24126999A JP2001062240A (ja) 1999-08-27 1999-08-27 混合ガスの濃度調整方法および濃度調整装置
JP24126999 1999-08-27

Publications (3)

Publication Number Publication Date
EP1078677A2 true EP1078677A2 (fr) 2001-02-28
EP1078677A3 EP1078677A3 (fr) 2002-01-16
EP1078677B1 EP1078677B1 (fr) 2004-08-25

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EP00115109A Expired - Lifetime EP1078677B1 (fr) 1999-08-27 2000-07-12 Procédé pour règler la concentration d'un melange gazeux

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US (1) US6387157B1 (fr)
EP (1) EP1078677B1 (fr)
JP (1) JP2001062240A (fr)
DE (1) DE60013212T2 (fr)

Cited By (3)

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Publication number Priority date Publication date Assignee Title
DE10353033A1 (de) * 2003-11-13 2005-06-09 Inficon Gmbh Verfahren zum Betrieb eines Wasserstoff-Testlecks
FR2898065A1 (fr) * 2006-03-01 2007-09-07 Air Liquide Controle du traitement d'un gaz hydrogene par voie membranaire
CN102071039A (zh) * 2010-12-16 2011-05-25 大连理工大学 一种提高浅冷回收油田伴生气轻烃效率的方法

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JP4769350B2 (ja) * 2000-09-22 2011-09-07 大陽日酸株式会社 希ガスの回収方法及び装置
DE10047262B4 (de) * 2000-09-23 2005-12-01 G.A.S. Energietechnologie Gmbh Verfahren zur Nutzung methanhaltiger Gase
DE60231600D1 (de) * 2001-01-25 2009-04-30 Ube Industries Verfahren und anlage zur trennung und rückgewinnung von halogengas
FR2829403B1 (fr) * 2001-09-11 2003-12-12 Air Liquide Procede de production par permeation, a partir d'un melange gazeux, d'au moins deux flux gazeux et installation de mise en oeuvre d'un tel procede
US6887300B2 (en) * 2003-01-24 2005-05-03 Cms Technology Holdings, Inc. Cyclic membrane separation process
US6866698B2 (en) * 2003-03-19 2005-03-15 Johnson Matthey Public Limited Company Hydrogen purification apparatus
US6986802B2 (en) * 2003-08-28 2006-01-17 Bp Corporation North America Inc. Selective separation of fluid compounds utilizing a membrane separation process
JP2006232649A (ja) * 2005-02-21 2006-09-07 Fukuhara Co Ltd 水素ガスの製造装置。
JP5013855B2 (ja) * 2006-12-27 2012-08-29 日本エア・リキード株式会社 ガス分離膜を用いたガス製造方法およびガス製造装置
FR2918978B1 (fr) * 2007-07-20 2010-02-12 Inst Francais Du Petrole Nouveau procede de purification d'hydrogene utilisant une combinaison d'unites de separation sur membranes
JP2009061420A (ja) * 2007-09-07 2009-03-26 Air Liquide Japan Ltd ガス成分および凝縮性成分の製造方法および製造システム
JP2014117687A (ja) * 2012-12-19 2014-06-30 Ube Ind Ltd ガス分離回収システムおよびガス分離回収方法
KR101838141B1 (ko) 2016-01-06 2018-03-14 한국과학기술연구원 고투과성기체 회수장치 및 방법
EP4282815A1 (fr) * 2022-05-25 2023-11-29 Basf Se Procédé de récupération de h2

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FR2731163A1 (fr) * 1995-03-03 1996-09-06 Air Liquide Procede et installation de separation d'un melange gazeux par permeation
EP0974389A2 (fr) * 1998-07-22 2000-01-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et dispositif pour la récupération d'un composant gazeux à partir d'un mélange de gaz

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10353033A1 (de) * 2003-11-13 2005-06-09 Inficon Gmbh Verfahren zum Betrieb eines Wasserstoff-Testlecks
FR2898065A1 (fr) * 2006-03-01 2007-09-07 Air Liquide Controle du traitement d'un gaz hydrogene par voie membranaire
WO2007099242A2 (fr) * 2006-03-01 2007-09-07 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Controle du traitement d'un gaz hydrogene par voie membranaire
WO2007099242A3 (fr) * 2006-03-01 2007-11-01 Air Liquide Controle du traitement d'un gaz hydrogene par voie membranaire
CN102071039A (zh) * 2010-12-16 2011-05-25 大连理工大学 一种提高浅冷回收油田伴生气轻烃效率的方法
CN102071039B (zh) * 2010-12-16 2013-06-19 大连理工大学 一种提高浅冷回收油田伴生气轻烃效率的方法

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DE60013212T2 (de) 2005-09-15
EP1078677B1 (fr) 2004-08-25
US6387157B1 (en) 2002-05-14
EP1078677A3 (fr) 2002-01-16
DE60013212D1 (de) 2004-09-30

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